Pyrolysis process for waste and old rubber

ABSTRACT

This invention is about a cracking technology of waste rubber, and the content of this technology is as following: the rubber mass with the catalyst were added in the cracking chamber and the cracking process of the raw material is finished. The main contents and weight percentage of catalyzer are as following: the aluminosilicate is from 35 to 50, the active alumina is from 15 to 30, the zinc oxide is from 10 to 20, the active argil is from 5 to 15, the kaoline is from 5 to 15, the weight ratio of catalyst and rubber is 2-7:1000; The cracking temperature is from 350 to 450° C. The rubber mass crack comparative downright in low temperature by using this combinatorial catalyst, that&#39;s because the temperature is controlled between 350 and 450° C., which commendably control the cracking process of the carbon chain of rubber. Moreover, more low carbon chain products can be gained for the symmetrical cracking. Therefore, the emerging ratio of the oil will become higher, the exhaust gas emission will become lower and the eligible emission will really come ture.

This application is the U.S. national phase of International ApplicationNo. PCT/CN2006/003500 filed 20 Dec. 2006 which designated the U.S., theentire contents of each of which is hereby incorporated by reference.

FIELD OF INVENTION

This invention is about a new cracking technology of waste rubber, whichis the key to produce oil by use of waste rubber.

BACKGROUND OF THE INVENTION

As is known, waste rubber can be re-produced into gasoline, diesel oiland others after being cracked, that not only gives out a good means fordisposal of the industrial rubbish, like rubber, etc. from waste tyresand so on in modern society, but also provides a new plan for theimprovement of decreasing resources and energy. However, at presenttime, almost all of present technologies usually use the hightemperature cracking technology, which break down the carbon chain ofthe rubber in the high temperature, and get the low carbon chain of oiland gas for recycling use. However, the cracking temperature commonlyneed up to 500□ in all of present technologies, what's more, someusually need up from 700 to 800□. Though the waste rubber could becracked completely at this temperature, the carbon chain was also brokendown excessively and gained the lower carbon chain of gaseous productsbecause of the high temperature. Accordingly, a huge gas processorshould be needed to treat with the follow-up product and some oilproduct could not be used directly for the bad quality. The gas producthas higher content of sulfur, which will pollute the environment whenusing. In order to gain the high cracking temperature, the crackingchamber needs enough quantity of heat, which costs much more fuel.However, the efficiency is much lower and it makes against to theindustrial production. Because of the cracking temperature is about 700°C., the quality of the carbon black, which was produced after thecracking process, will become bad and it's hard to revert. Moreover, therecycle of it will become hard.

Thus it can be seen that a good many problems and shortages exist inpresent technologies of cracking waste rubber, such as overmuchdepending on the energy, the income is lower and polluting the humanliving environment because of the technical problem.

SUMMARY OF THE INVENTION

To the shortages existing in present technologies, this inventionprovides a cracking technology of waste rubber, and the main content ofit is as following: the breaking up technology of waste rubber, thecontinuously cracking technology, the separating and fractionationtechnology of the oil-gas after cracking, the purification anddecontamination technology of the carbon black, the comprehensiveutilization technology of the combustible gas and the purifyingtreatment technology of tail gas. Adopting the technology providing bythis invention, the cracking temperature will become lower, the cost ofenergy consumption can be reduced, the quality of cracking product canbe increased and the pollution of environment will become lower.

The specific content of this technology is adding the rubber mass withthe catalyst to the cracking chamber, and next the cracking process ofthe raw material is finished. The main contents and weight percentage ofcatalyzer are as following: the aluminosilicate is from 35 to 50 wt %,the active alumina is from 15 to 30 wt %, the zinc oxide is from 10 to20 wt %, the active argil is from 5 to 15 wt % and the kaoline is from 5to 15 wt %. The weight ratio of catalyst and rubber is 2-7:1000. Thecracking temperature is from 350 to 450° C. The rubber mass crackcompletely in low temperature by using this combinatorial catalyst,that's because the temperature is controlled between 350 and 450° C.,and that method commendably controlled the cracking process of thecarbon chain of rubber. Moreover, more low carbon chain products can begained by the symmetrical cracking. Therefore, the emersion ratio of theoil will become higher, the exhaust gas emission will become lower andthe eligible emission will really come ture.

The aluminosilicate molecular sieve was used in this technology, and themain use of it is the model Y, 3A, 4A, and 5A.

When cracking, the heating temperature difference, which is thetemperature difference in different part of cracking chamber withoutadding the raw material, should be controlled at or within 10° C.Ordinarily, that temperature difference is between the inlet orifice anddischarge hole less than 10° C. Moreover, at that temperature, it notonly reaches the needing temperature for the cracking of rubber, butalso ensures the cracking process steadily continuously progressingbecause of the temperature difference is less than or equal to 10° C.What's more, the quality of the cracking rubber can be ensured and theoil-gas ratio will be optimal.

The cracking time can be set according to the requirement when cracking.Usually, it can be set at 10 and 70 minutes or shorter or longer.However, considering the production efficiency and cracking effect, thecracking time can be controlled between 20 and 60 minutes. All of thathelps ensure the cracking time becomes shorter, compared to the hightemperature cracking. On this basis, the cost of energy consumption willbe reduced, much more time will be saved when treating large volumes ofwaste rubber, and the quality of cracking products will be ensured atthe same time the treatment efficiency will be improved.

In the invention, the cracking temperature can be controlled furtherfrom 370 to 420° C. At this temperature, the cracking effect of rawmaterial and the quality of the oil are better. Moreover, the quality ofexhaust gas can be improved. On this basis, if controlling the crackingtemperature from 380 to 390° C., the effect is better. What's more, atthis temperature, the rubber can crack completely, the liquid-gas ratiogetting by cracking is best, the quality of oil product is optimal, theseparation of the gasoline and diesel oil is thorough at the same timethe content of impurity is lowest, the volume of the emanatingcombustible gas is fewer, and it can predigest the follow-up process orreduce the technical requirement for the follow-up process.

The heating mode can use the present methods in the cracking process.However, the best is using temperature controlled gaseity, liquid stateor solid state carrier, such as the heating liquid molten salt. In orderto achieve the heating request, the heating temperature of heat carriercan be controlled between 380 and 490° C., which ensures the crackingtemperature in the cracking chamber satisfies the request. Using of thisheating method can provide a steady temperature circumstance in crackingchamber and ensure the cracking process progressing steadily. What'smore, controlling the temperature at this scope, the inner temperatureof cracking chamber can reach the requested temperature for the rubbercracking.

When the cracking process is finished, the cracking gas can getcombustible gas and oil by fractionating. According to the differentrequest, the combustible gas can be directly expelled out or storedafter desulfurized.

The combustible gas can be directly expelled into the heating furnace,which supplying the heat to the cracking process. And it also can bestored for other use. All of these methods can make the best use ofcombustible gas. The combustible gas will make exhaust gas again afterburning in the heating furnace, and this exhaust gas can be expelled outdirectly. However, if it falls short of the stated request, a secondarytreating will be needed. The secondary treating can adopt the followingmode: refrigerating the exhaust gas below 70° C., then dealing with itby the transaction layer of active carbon, active fiber and zeolitemolecular sieve respectively. At this temperature the contamination inthe exhaust gas will be adsorbed and ensure it reach the emissionstandard. What's more, the refrigerating temperature can be furthercontrolled between 40 and 55° C., because it will be better foradsorbing the contamination in exhaust gas, and the equipment cost willbe lower. In this invention, the secondary treating technology will beaccomplished by the present exhaust gas processing equipment.

When the exhaust gas passes the different transaction layer in secondarytreating, the through speed of the exhaust gas should be controlledbetween 0.1 and 1 m/s, which ensure the contamination being adsorbedadequately. By reducing the through speed of the exhaust gas, thecontamination adsorbed in the transaction layer is better. Therefore,the exhaust gas emission can reach the emission standard. Moreover, therefrigerating technology can use the present gas cooling technology andequipment.

The solid state product, which is produced after cracking process,contains carbon black. And it can be made into carbon black by theprocedure of magnetic separation, comminution and selection bywinnowing. According to different demand, a series of differentthickness carbon black can be gained by the above-mentioned treatingmethod, such as more than 650 mesh. After accomplishing theaforementioned process, the stearic acid is added into the carbon black.And it can be mixed with the remaining components, into zinc stearate.What's more, the zinc stearate can reinforce the role of carbon black.That's because the zinc stearate can form the zinc stearate, which is areinforcing agent, by reacting with zinc oxide.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is the process flow diagram of the example 84 of this invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

The following examples are only the further explanation of the technicalcontent of this invention, but not the confinement for this invention.

EXAMPLE 1

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, which is the aluminosilicate. Thealuminosilicate is 35 wt %, the active alumina is 15 wt %, the zincoxide is 10 wt %, the active argil is 5 wt % and the kaoline is 5 wt %.The weight ratio of catalyst and rubber is 2:1000, and then the mixtureis transported into the reactor for the cracking reaction. The crackingtemperature is 450° C., the cracking time is 10 minutes and the heatingtemperature difference in the cracking chamber is 10° C. The liquidstate product can be made into needing oil by fractionating. Moreover,the gas state and solid state products can be given up directly ortreated further by the conventional method. The rest parts exercise thesame as the existing technologies.

EXAMPLE 2

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C., thecracking time is 80 minutes and the heating temperature difference inthe cracking chamber is 9° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The rest parts exercise the same as the existing technologies.

EXAMPLE 3

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C., thecracking time is 50 minutes and the heating temperature difference inthe cracking chamber is 9° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The rest parts exercise the same as the existing technologies.

EXAMPLE 4

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 36. Theactive alumina is 16 wt %, the zinc oxide is 11 wt %, the active argilis 6 wt % and the kaoline is 6 wt %. The weight ratio of catalyst andrubber is 4:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 370° C., thecracking time is 60 minutes and the heating temperature difference inthe cracking chamber is 8° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The rest parts exercise the same as the existing technologies.

EXAMPLE 5

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 37. Theactive alumina is 17 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 4.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 420° C., thecracking time is 20 minutes and the heating temperature difference inthe cracking chamber is 6° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The rest parts exercise the same as the existing technologies.

EXAMPLE 6

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 38. Theactive alumina is 18 wt %, the zinc oxide is 13 wt %, the active argilis 8 wt % and the kaoline is 7 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 380° C., thecracking time is 40 minutes and the heating temperature difference inthe cracking chamber is 7° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The rest parts exercise the same as the existing technologies.

EXAMPLE 7

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 39. Theactive alumina is 19 wt %, the zinc oxide is 14 wt %, the active argilis 10 wt % and the kaoline is 9 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 390° C., thecracking time is 30 minutes and the heating temperature difference inthe cracking chamber is 10° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up, directly or treated further by theconventional method. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 8

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 40. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 9 wt % and the kaoline is 10 wt %. The weight ratio of catalyst andrubber is 2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 410° C., thecracking time is 15 minutes and the heating temperature difference inthe cracking chamber is 1° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. What's more, the temperature of the heat carrier can be adjustedat 435° C., which satisfy the temperature request for cracking. The restparts exercise the same as the existing technologies.

EXAMPLE 9

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C., thecracking time is 80 minutes and the heating temperature difference inthe cracking chamber is 2° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. What's more, the temperature of the heat carrier can be adjustedat 380° C., which satisfy the temperature request for cracking. The restparts exercise the same as the existing technologies.

EXAMPLE 10

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 5:1000, and then the mixture is transported intothe reactor for the cracking reaction. The cracking temperature is 350°C. and the cracking time is 50 minutes. The liquid state product can bemade into needing oil by fractionating. Moreover, the gas state andsolid state products can be given up directly or treated further by theconventional method. What's more, the temperature of the heat carriercan be adjusted at 385° C., which satisfy the temperature request forcracking. The rest parts exercise the same as the existing technologies.

EXAMPLE 11

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 41. Theactive alumina is 21 wt %, the zinc oxide is 16 wt %, the active argilis 12 wt % and the kaoline is 12 wt %. The weight ratio of catalyst andrubber is 3.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 370° C. and thecracking time is 55 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. What's more, the temperature of the heat carrier can be adjustedat 405° C., which satisfy the temperature request for cracking. The restparts exercise the same as the existing technologies.

EXAMPLE 12

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 42. Theactive alumina is 22 wt %, the zinc oxide is 17 wt %, the active argilis 11 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 6.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 420° C. and thecracking time is 20 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. What's more, the temperature of the heat carrier can be adjustedat 445° C., which satisfy the temperature request for cracking. The restparts exercise the same as the existing technologies.

EXAMPLE 13

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 44. Theactive alumina is 24 wt %, the zinc oxide is 19 wt %, the active argilis 13 wt % and the kaoline is 12 wt %. The weight ratio of catalyst andrubber is 5.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 380° C. and thecracking time is 45 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. What's more, the temperature of the heat carrier can be adjustedat 425° C., which satisfy the temperature request for cracking. The restparts exercise the same as the existing technologies.

EXAMPLE 14

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 45. Theactive alumina is 25 wt %, the zinc oxide is 20 wt %, the active argilis 14 wt % and the kaoline is 13 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 2.5:1000, and then the mixture is transportedinto the reactor for the cracking reaction. The cracking temperature is390° C. and the cracking time is 30 minutes. The liquid state productcan be made into needing oil by fractionating. Moreover, the gas stateand solid state products can be given up directly or treated further bythe conventional method. What's more, the temperature of the heatcarrier can be adjusted at 425° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 15

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 35. Theactive alumina is 15 wt %, the zinc oxide is 10 wt %, the active argilis 5 wt % and the kaoline is 5 wt %. The weight ratio of catalyst andrubber is 2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 450° C. and thecracking time is 10 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 16

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C. and thecracking time is 75 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 17

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C. and thecracking time is 50 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 18

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 46. Theactive alumina is 26 wt %, the zinc oxide is 20 wt %, the active argilis 13 wt % and the kaoline is 14 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 3.5:1000, and then the mixture is transportedinto the reactor for the cracking reaction. The cracking temperature is370° C., the cracking time is 60 minutes and the heating temperaturedifference in the cracking chamber is 2° C. The liquid state product canbe made into needing oil by fractionating. Moreover, the gas state andsolid state products can be given up directly or treated further by theconventional method. In this example, the heat carrier was heated at thefurnace and transported into the reactor. Then the heat carrier supplieda quantity of heat for the cracking process. The cracking gas can getcombustible gas and oil by fractionating. What's more, the combustiblegas, which was desulfurized by the sodium hydroxide, can be directlyexpelled into or stored and then expelled into the heating furnace forburning. The rest parts exercise the same as the existing technologies.

EXAMPLE 19

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 47. Theactive alumina is 27 wt %, the zinc oxide is 15 wt %, the active argilis 15 wt % and the kaoline is 7 wt %. The weight ratio of catalyst andrubber is 2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 420° C. and thecracking time is 20 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace, andfollowing was transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the sodium hydroxide, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 20

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 48. Theactive alumina is 28 wt %, the zinc oxide is 15 wt %, the active argilis 5 wt % and the kaoline is 15 wt %. The weight ratio of catalyst andrubber is 4:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 380° C. and thecracking time is 40 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 21

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 49. Theactive alumina is 29 wt %, the zinc oxide is 19 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 4.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 390° C. and thecracking time is 30 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 22

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 50. Theactive alumina is 30 wt %, the zinc oxide is 20 wt %, the active argilis 15 wt % and the kaoline is 5 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 2:1000, and then the mixture is transported intothe reactor for the cracking reaction. The cracking temperature is 450°C., the cracking time is 10 minutes and the heating temperaturedifference in the cracking chamber is 5° C. The liquid state product canbe made into needing oil by fractionating. Moreover, the gas state andsolid state products can be given up directly or treated further by theconventional method. In this example, the heat carrier was heated at thefurnace and transported into the reactor. Then the heat carrier supplieda quantity of heat for the cracking process. The cracking gas can getcombustible gas and oil by fractionating. Moreover, the combustible gas,which was desulfurized by the conventional desulfurization method, canbe directly expelled into or stored and then expelled into the heatingfurnace for burning. What's more, the temperature of the heat carriercan be adjusted at 485° C., which satisfy the temperature request forcracking. The rest parts exercise the same as the existing technologies.

EXAMPLE 23

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C. and thecracking time is 80 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. Moreover, the temperature of the heat carrier canbe adjusted at 395° C., which satisfy the temperature request forcracking, and the heat carrier is the gas one. The rest parts exercisethe same as the existing technologies.

EXAMPLE 24

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C., thecracking time is 50 minutes and the heating temperature difference inthe cracking chamber is 4° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning.Moreover, the temperature of the heat carrier can be adjusted at 390°C., which satisfy the temperature request for cracking, and the heatcarrier is the solid one. The rest parts exercise the same as theexisting technologies.

EXAMPLE 25

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 35. Theactive alumina is 28 wt %, the zinc oxide is 15 wt %, the active argilis 11 wt % and the kaoline is 9 wt %. The weight ratio of catalyst andrubber is 2.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 381° C. and thecracking time is 55 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning.Moreover, the temperature of the heat carrier can be adjusted at 405°C., which satisfy the temperature request for cracking. The rest partsexercise the same as the existing technologies.

EXAMPLE 26

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 37. Theactive alumina is 25 wt %, the zinc oxide is 18 wt %, the active argilis 12 wt % and the kaoline is 14 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 5:1000, and then the mixture is transported intothe reactor for the cracking reaction. The cracking temperature is 382°C. and the cracking time is 25 minutes. The liquid state product can bemade into needing oil by fractionating. Moreover, the gas state andsolid state products can be given up directly or treated further by theconventional method. In this example, the heat carrier was heated at thefurnace and transported into the reactor. Then the heat carrier supplieda quantity of heat for the cracking process. The cracking gas can getcombustible gas and oil by fractionating. What's more, the combustiblegas, which was desulfurized by the sodium hydroxide, can be directlyexpelled into or stored and then expelled into the heating furnace forburning. Moreover, the temperature of the heat carrier can be adjustedat 405° C., which satisfy the temperature request for cracking. The restparts exercise the same as the existing technologies.

EXAMPLE 27

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 36. Theactive alumina is 15 wt %, the zinc oxide is 12 wt %, the active argilis 15 wt % and the kaoline is 9 wt %. The weight ratio of catalyst andrubber is 2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 383° C. and thecracking time is 40 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning.Moreover, the temperature of the heat carrier can be adjusted at 408°C., which satisfy the temperature request for cracking. The rest partsexercise the same as the existing technologies.

EXAMPLE 28

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 38. Theactive alumina is 22 wt %, the zinc oxide is 16 wt %, the active argilis 10 wt % and the kaoline is 12 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 384° C. and thecracking time is 35 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning.Moreover, the temperature of the heat carrier can be adjusted at 410°C., which satisfy the temperature request for cracking. The rest partsexercise the same as the existing technologies.

EXAMPLE 29

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 35. Theactive alumina is 15 wt %, the zinc oxide is 10 wt %, the active argilis 5 wt % and the kaoline is 5 wt %. The weight ratio of catalyst andrubber is 2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 450° C. and thecracking time is 10 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The exhaust gas, making by burning the combustiblegas, should be treated again and exhausted out. What's more, thesecondary treating can adopt the following mode: refrigerating theexhaust gas below 70° C., then deal with it by the transaction layer ofactive carbon, active fiber and zeolite molecular sieve, respectively.The rest parts exercise the same as the existing technologies.

EXAMPLE 30

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C. and thecracking time is 80 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The exhaust gas, making by burning the combustiblegas, should be treated again and exhausted out. What's more, thesecondary treating can adopt the following mode: refrigerating theexhaust gas below 68° C., then deal with it by the transaction layer ofactive carbon, active fiber and zeolite molecular sieve, respectively.The rest parts exercise the same as the existing technologies.

EXAMPLE 31

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 7:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C. and thecracking time is 50 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The exhaust gas, making by burning the combustiblegas, should be treated again and exhausted out. What's more, thesecondary treating can adopt the following mode: refrigerating theexhaust gas below 65° C., then deal with it by the transaction layer ofactive carbon, active fiber and zeolite molecular sieve respectively,and the through speed of exhaust gas was controlled at 0.1 m/s. The restparts exercise the same as the existing technologies.

EXAMPLE 32

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 40. Theactive alumina is 27 wt %, the zinc oxide is 19 wt %, the active argilis 6 wt % and the kaoline is 5 wt %. The weight ratio of catalyst andrubber is 6.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 385° C., thecracking time is 55 minutes and the heating temperature difference inthe cracking chamber is 10° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning. Theexhaust gas, making by burning the combustible gas, should be treatedagain and exhausted out. What's more, the secondary treating can adoptthe following mode: refrigerating the exhaust gas below 60° C., thendeal with it by the transaction layer of active carbon, active fiber andzeolite molecular sieve respectively, and the through speed of exhaustgas was controlled at 0.2 m/s. The rest parts exercise the same as theexisting technologies.

EXAMPLE 33

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 37. Theactive alumina is 28 wt %, the zinc oxide is 11 wt %, the active argilis 5 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 4.8:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 486° C., thecracking time is 35 minutes and the heating temperature difference inthe cracking chamber is 3° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning. Theexhaust gas, making by burning the combustible gas, should be treatedagain and exhausted out. What's more, the secondary treating can adoptthe following mode: refrigerating the exhaust gas below 50° C., thendeal with it by the transaction layer of active carbon, active fiber andzeolite molecular sieve respectively, and the following rate of exhaustgas was controlled at 0.4 m/s. The rest parts exercise the same as theexisting technologies.

EXAMPLE 34

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 35. Theactive alumina is 30 wt %, the zinc oxide is 20 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 3.2:1000, and then the mixture is transportedinto the reactor for the cracking reaction. The cracking temperature is387° C. and the cracking time is 40 minutes. The liquid state productcan be made into needing oil by fractionating. Moreover, the gas stateand solid state products can be given up directly or treated further bythe conventional method. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the conventionaldesulfurization method, can be directly expelled into or stored and thenexpelled into the heating furnace for burning. The exhaust gas, makingby burning the combustible gas, should be treated again and exhaustedout. What's more, the secondary treating can adopt the following mode:refrigerating the exhaust gas below 42° C., then deal with it by thetransaction layer of active carbon, active fiber and zeolite molecularsieve respectively, and the through speed of exhaust gas was controlledat 0.5 m/s. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 35

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 39. Theactive alumina is 21 wt %, the zinc oxide is 13 wt %, the active argilis 11 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 2.8:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 388° C., thecracking time is 35 minutes and the heating temperature difference inthe cracking chamber is 7° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The exhaust gas, making by burning the combustiblegas, should be treated again and exhausted out. What's more, thesecondary treating can adopt the following mode: refrigerating theexhaust gas below 40° C., then deal with it by the transaction layer ofactive carbon, active fiber and zeolite molecular sieve respectively,and the following rate of exhaust gas was controlled at 0.6 m/s. Therest parts exercise the same as the existing technologies.

EXAMPLE 36

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 43. Theactive alumina is 25 wt %, the zinc oxide is 10 wt %, the active argilis 8 wt % and the kaoline is 14 wt %. The weight ratio of catalyst andrubber is 2.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 389° C. and thecracking time is 15 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The exhaust gas, making by burning the combustiblegas, should be treated again and exhausted out. What's more, thesecondary treating can adopt the following mode: refrigerating theexhaust gas below 40° C., then deal with it by the transaction layer ofactive carbon, active fiber and zeolite molecular sieve respectively,and the through speed of exhaust gas was controlled at 0.7 m/s.Moreover, the temperature of the heat carrier can be adjusted at 430°C., which satisfy the temperature request for cracking. The rest partsexercise the same as the existing technologies.

EXAMPLE 37

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C. and thecracking time is 80 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the conventional desulfurization method, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The exhaust gas, making by burning the combustiblegas, should be treated again and exhausted out. What's more, thesecondary treating can adopt the following mode: refrigerating theexhaust gas below 35° C., then deal with it by the transaction layer ofactive carbon, active fiber and zeolite molecular sieve respectively,and the following rate of exhaust gas was controlled at 0.8 m/s.Moreover, the temperature of the heat carrier can be adjusted at 395°C., which satisfy the temperature request for cracking. The rest partsexercise the same as the existing technologies.

EXAMPLE 38

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C., thecracking time is 50 minutes and the heating temperature difference inthe cracking chamber is 6° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning. Theexhaust gas, making by burning the combustible gas, should be treatedagain and exhausted out. What's more, the secondary treating can adoptthe following mode: refrigerating the exhaust gas below 58° C., thendeal with it by the transaction layer of active carbon, active fiber andzeolite molecular sieve respectively, and the through speed of exhaustgas was controlled at 0.9 m/s. Moreover, the temperature of the heatcarrier can be adjusted at 390° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 39

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 44. Theactive alumina is 27 wt %, the zinc oxide is 12 wt %, the active argilis 10 wt % and the kaoline is 14 wt %. The weight ratio of catalyst andrubber is 3.4:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 390° C., thecracking time is 58 minutes and the heating temperature difference inthe cracking chamber is 1° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning. Theexhaust gas, making by burning the combustible gas, should be treatedagain and exhausted out. What's more, the secondary treating can adoptthe following mode: refrigerating the exhaust gas below 45° C., thendeal with it by the transaction layer of active carbon, active fiber andzeolite molecular sieve respectively, and the following rate of exhaustgas was controlled at 1 m/s. Moreover, the temperature of the heatcarrier can be adjusted at 425° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 40

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 5:1000, and then the mixture is transported intothe reactor for the cracking reaction. The cracking temperature is 395°C. and the cracking time is 20 minutes. The liquid state product can bemade into needing oil by fractionating. Moreover, the gas state andsolid state products can be given up directly or treated further by theconventional method. In this example, the heat carrier was heated at thefurnace and transported into the reactor. Then the heat carrier supplieda quantity of heat for the cracking process. The cracking gas can getcombustible gas and oil by fractionating. What's more, the combustiblegas, which was desulfurized by the sodium hydroxide, can be directlyexpelled into or stored and then expelled into the heating furnace forburning. The exhaust gas, making by burning the combustible gas, shouldbe treated again and exhausted out. What's more, the secondary treatingcan adopt the following mode: refrigerating the exhaust gas below 55°C., then deal with it by the transaction layer of active carbon, activefiber and zeolite molecular sieve respectively, and the through speed ofexhaust gas was controlled at 1.1 m/s. Moreover, the temperature of theheat carrier can be adjusted at 450° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 41

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 43. Theactive alumina is 15 wt %, the zinc oxide is 20 wt %, the active argilis 10 wt % and the kaoline is 15 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 6.5:1000, and then the mixture is transportedinto the reactor for the cracking reaction. The cracking temperature is400° C. and the cracking time is 35 minutes. The liquid state productcan be made into needing oil by fractionating. Moreover, the gas stateand solid state products can be given up directly or treated further bythe conventional method. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the sodium hydroxide, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. The exhaust gas, making by burning the combustiblegas, should be treated again and exhausted out. What's more, thesecondary treating can adopt the following mode: refrigerating theexhaust gas below 48° C., then deal with it by the transaction layer ofactive carbon, active fiber and zeolite molecular sieve respectively,and the following rate of exhaust gas was controlled at 0.3 m/s.Moreover, the temperature of the heat carrier can be adjusted at 450°C., which satisfy the temperature request for cracking. The rest partsexercise the same as the existing technologies.

EXAMPLE 42

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 37. Theactive alumina is 20 wt %, the zinc oxide is 20 wt %, the active argilis 6 wt % and the kaoline is 9 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 405° C. and thecracking time is 30 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. In this example, the heat carrier was heated at the furnace andtransported into the reactor. Then the heat carrier supplied a quantityof heat for the cracking process. The cracking gas can get combustiblegas and oil by fractionating. What's more, the combustible gas, whichwas desulfurized by the sodium hydroxide, can be directly expelled intoor stored and then expelled into the heating furnace for burning. Theexhaust gas, making by burning the combustible gas, should be treatedagain and exhausted out. What's more, the secondary treating can adoptthe following mode: refrigerating the exhaust gas below 52° C., thendeal with it by the transaction layer of active carbon, active fiber andzeolite molecular sieve respectively, and the through speed of exhaustgas was controlled at 0.5 m/s. Moreover, the temperature of the heatcarrier can be adjusted at 440° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 43

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 35. Theactive alumina is 15 wt %, the zinc oxide is 10 wt %, the active argilis 5 wt % and the kaoline is 5 wt %. The weight ratio of catalyst andrubber is 2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 450° C., thecracking time is 10 minutes and the heating temperature difference inthe cracking chamber is 10° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. The restparts exercise the same as the existing technologies.

EXAMPLE 44

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C. and thecracking time is 80 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. The restparts exercise the same as the existing technologies.

EXAMPLE 45

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C. and thecracking time is 50 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. The restparts exercise the same as the existing technologies.

EXAMPLE 46

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 36. Theactive alumina is 21 wt %, the zinc oxide is 14 wt %, the active argilis 7 wt % and the kaoline is 7 wt %. The steel wires were separated fromrubber by drawing the waste rubber into thread, and then the big piecesof rubber were broken up into granule. The weight ratio of catalyst andrubber is 6:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 410° C. and thecracking time is 45 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. The restparts exercise the same as the existing technologies.

EXAMPLE 47

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 38. Theactive alumina is 29 wt %, the zinc oxide is 14 wt %, the active argilis 10 wt % and the kaoline is 12 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 415° C. and thecracking time is 25 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. The restparts exercise the same as the existing technologies.

EXAMPLE 48

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 49. Theactive alumina is 17 wt %, the zinc oxide is 15 wt %, the active argilis 14 wt % and the kaoline is 6 wt %. The weight ratio of catalyst andrubber is 2.2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 420° C. and thecracking time is 35 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. The restparts exercise the same as the existing technologies.

EXAMPLE 49

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 14 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 6.7:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 425° C. and thecracking time is 34 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. The restparts exercise the same as the existing technologies.

EXAMPLE 50

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 38. Theactive alumina is 25 wt %, the zinc oxide is 13 wt %, the active argilis 15 wt % and the kaoline is 15 wt %. The weight ratio of catalyst andrubber is 5.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 430° C. and thecracking time is 25 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. Moreover,the temperature of the heat carrier can be adjusted at 455° C., whichsatisfy the temperature request for cracking. The rest parts exercisethe same as the existing technologies.

EXAMPLE 51

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight ratio is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C. and thecracking time is 80 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. Moreover,the temperature of the heat carrier can be adjusted at 395° C., whichsatisfy the temperature request for cracking. The rest parts exercisethe same as the existing technologies.

EXAMPLE 52

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 2.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C., thecracking time is 50 minutes and the heating temperature difference inthe cracking chamber is 5° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. Moreover,the temperature of the heat carrier can be adjusted at 380° C., whichsatisfy the temperature request for cracking. The rest parts exercisethe same as the existing technologies.

EXAMPLE 53

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 50. Theactive alumina is 21 wt %, the zinc oxide is 17 wt %, the active argilis 11 wt % and the kaoline is 13 wt %. The weight ratio of catalyst andrubber is 4.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 435° C., thecracking time is 25 minutes and the heating temperature difference inthe cracking chamber is 4° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. Moreover,the temperature of the heat carrier can be adjusted at 460° C., whichsatisfy the temperature request for cracking. The rest parts exercisethe same as the existing technologies.

EXAMPLE 54

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 37. Theactive alumina is 28 wt %, the zinc oxide is 18 wt %, the active argilis 8 wt % and the kaoline is 11 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 5:1000, and then the mixture is transported intothe reactor for the cracking reaction. The cracking temperature is 440°C., the cracking time is 20 minutes and the heating temperaturedifference in the cracking chamber is 8° C. The liquid state product canbe made into needing oil by fractionating. Moreover, the gas state andsolid state products can be given up directly or treated further by theconventional method. The solid state product, which produced aftercracking, contains carbon black. And it can be made into carbon black bythe procedure of magnetic separation, comminution and selection bywinnowing. Moreover, the temperature of the heat carrier can be adjustedat 465° C., which satisfy the temperature request for cracking. The restparts exercise the same as the existing technologies.

EXAMPLE 55

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 40. Theactive alumina is 26 wt %, the zinc oxide is 17 wt %, the active argilis 14 wt % and the kaoline is 6 wt %. The weight ratio of catalyst andrubber is 6:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 445° C. and thecracking time is 15 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. Moreover,the temperature of the heat carrier can be adjusted at 480° C., whichsatisfy the temperature request for cracking. The rest parts exercisethe same as the existing technologies.

EXAMPLE 56

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 43. Theactive alumina is 22 wt %, the zinc oxide is 11 wt %, the active argilis 5 wt % and the kaoline is 14 wt %. The weight ratio of catalyst andrubber is 4:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 450° C. and thecracking time is 10 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the gas state and solid stateproducts can be given up directly or treated further by the conventionalmethod. The solid state product, which produced after cracking, containscarbon black. And it can be made into carbon black by the procedure ofmagnetic separation, comminution and selection by winnowing. Moreover,the temperature of the heat carrier can be adjusted at 490° C., whichsatisfy the temperature request for cracking. The rest parts exercisethe same as the existing technologies.

EXAMPLE 57

The components and weight ratio of the catalyzer are as following: themodel of molecular sieve is 4A, and the weight percentage is 44. Theactive alumina is 15 wt %, the zinc oxide is 10 wt %, the active argilis 5 wt % and the kaoline is 5 wt %. The steel wires were separated fromrubber by drawing the waste rubber into thread, and then the big piecesof rubber were broken up into granule. The weight ratio of catalyst andrubber is 2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 450° C. and thecracking time is 10 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the conventionaldesulfurization method, can be directly expelled into or stored and thenexpelled into the heating furnace for burning. The rest parts exercisethe same as the existing technologies.

EXAMPLE 58

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 3:1000, and then the mixture is transported intothe reactor for the cracking reaction. The cracking temperature is 350°C., the cracking time is 80 minutes and the heating temperaturedifference in the cracking chamber is 2° C. The liquid state product canbe made into needing oil by fractionating. Moreover, the solid stateproduct, which produced after cracking, contains carbon black. And itcan be made into carbon black, which can pass the screen of 650 mesh, bythe procedure of magnetic separation, comminution and selection bywinnowing. In this example, the heat carrier was heated at the furnaceand transported into the reactor. Then the heat carrier supplied aquantity of heat for the cracking process. The cracking gas can getcombustible gas and oil by fractionating. What's more, the combustiblegas, which was desulfurized by the conventional desulfurization method,can be directly expelled into or stored and then expelled into theheating furnace for burning. The rest parts exercise the same as theexisting technologies.

EXAMPLE 59

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 45. Theactive alumina is 30 wt %, the zinc oxide is 19 wt %, the active argilis 15 wt % and the kaoline is 15 wt %. The weight ratio of catalyst andrubber is 5.8:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 355° C. and thecracking time is 75 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 700 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. Afteraccomplishing the aforementioned process, adding the carbon black intothe stearic acid. And make it, mixing with the remanent components, intozinc stearate, which can reinforce the role of carbon black. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the conventional desulfurization method, can be directly expelledinto or stored and then expelled into the heating furnace for burning.The rest parts exercise the same as the existing technologies.

EXAMPLE 60

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 10 wt %, the active argilis 5 wt % and the kaoline is 15 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 7:1000, and then the mixture is transported intothe reactor for the cracking reaction. The cracking temperature is 360°C. and the cracking time is 60 minutes. The liquid state product can bemade into needing oil by fractionating. Moreover, the solid stateproduct, which produced after cracking, contains carbon black. And itcan be made into carbon black by the procedure of magnetic separation,comminution and selection by winnowing. After accomplishing theaforementioned process, adding the carbon black into the stearic acid.And make it, mixing with the remanent components, into zinc stearate,which can reinforce the role of carbon black. In this example, the heatcarrier was heated at the furnace and transported into the reactor. Thenthe heat carrier supplied a quantity of heat for the cracking process.The cracking gas can get combustible gas and oil by fractionating.What's more, the combustible gas, which was desulfurized by the sodiumhydroxide, can be directly expelled into or stored and then expelledinto the heating furnace for burning. The rest parts exercise the sameas the existing technologies.

EXAMPLE 61

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 45. Theactive alumina is 22 wt %, the zinc oxide is 20 wt %, the active argilis 7 wt % and the kaoline is 10 wt %. The weight ratio of catalyst andrubber is 6.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 365° C. and thecracking time is 55 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 650 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. Afteraccomplishing the aforementioned process, adding the carbon black intothe stearic acid. And make it, mixing with the remanent components, intozinc stearate, which can reinforce the role of carbon black. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the sodium hydroxide, can be directly expelled into or stored andthen expelled into the heating furnace for burning. The rest partsexercise the same as the existing technologies.

EXAMPLE 62

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 49. Theactive alumina is 29 wt %, the zinc oxide is 19 wt %, the active argilis 14 wt % and the kaoline is 15 wt %. The weight ratio of catalyst andrubber is 2:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 370° C. and thecracking time is 50 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the conventionaldesulfurization method, can be directly expelled into or stored and thenexpelled into the heating furnace for burning. The rest parts exercisethe same as the existing technologies.

EXAMPLE 63

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 36. Theactive alumina is 27 wt %, the zinc oxide is 15 wt %, the active argilis 5 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 375° C., thecracking time is 45 minutes and the heating temperature difference inthe cracking chamber is 5° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. After accomplishing the aforementioned process,adding the carbon black into the stearic acid. And make it, mixing withthe remanent components, into zinc stearate, which can reinforce therole of carbon black. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the conventionaldesulfurization method, can be directly expelled into or stored and thenexpelled into the heating furnace for burning. The rest parts exercisethe same as the existing technologies.

EXAMPLE 64

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 35. Theactive alumina is 20 wt %, the zinc oxide is 10 wt %, the active argilis 5 wt % and the kaoline is 5 wt %. The steel wires were separated fromrubber by drawing the waste rubber into thread, and then the big piecesof rubber were broken up into granule. The weight ratio of catalyst andrubber is 7:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 380° C., thecracking time is 40 minutes and the heating temperature difference inthe cracking chamber is 6° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 650 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. Afteraccomplishing the aforementioned process, adding the carbon black intothe stearic acid. And make it, mixing with the remanent components, intozinc stearate, which can reinforce the role of carbon black. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the conventional desulfurization method, can be directly expelledinto or stored and then expelled into the heating furnace for burning.Moreover, the temperature of the heat carrier can be adjusted at 415°C., which satisfy the temperature request for cracking. The rest partsexercise the same as the existing technologies.

EXAMPLE 65

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 40. Theactive alumina is 28 wt %, the zinc oxide is 20 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 5.3:1000, and then the mixture is transportedinto the reactor for the cracking reaction. The cracking temperature is360° C. and the cracking time is 75 minutes. The liquid state productcan be made into needing oil by fractionating. Moreover, the solid stateproduct, which produced after cracking, contains carbon black. And itcan be made into carbon black by the procedure of magnetic separation,comminution and selection by winnowing. In this example, the heatcarrier was heated at the furnace and transported into the reactor. Thenthe heat carrier supplied a quantity of heat for the cracking process.The cracking gas can get combustible gas and oil by fractionating.What's more, the combustible gas, which was desulfurized by theconventional desulfurization method, can be directly expelled into orstored and then expelled into the heating furnace for burning. Moreover,the temperature of the heat carrier can be adjusted at 390° C., whichsatisfy the temperature request for cracking. The rest parts exercisethe same as the existing technologies.

EXAMPLE 66

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 35. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 14 wt % and the kaoline is 12 wt %. The weight ratio of catalyst andrubber is 6.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C. and thecracking time is 60 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the sodium hydroxide, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. Moreover, the temperature of the heat carrier canbe adjusted at 385° C., which satisfy the temperature request forcracking. The rest parts exercise the same as the existing technologies.

EXAMPLE 67

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 35. Theactive alumina is 30 wt %, the zinc oxide is 20 wt %, the active argilis 10 wt % and the kaoline is 15 wt %. The steel wires were separatedfrom rubber by drawing the waste rubber into thread, and then the bigpieces of rubber were broken up into granule. The weight ratio ofcatalyst and rubber is 3.5:1000, and then the mixture is transportedinto the reactor for the cracking reaction. The cracking temperature is370° C. and the cracking time is 60 minutes. The liquid state productcan be made into needing oil by fractionating. Moreover, the solid stateproduct, which produced after cracking, contains carbon black. And itcan be made into carbon black by the procedure of magnetic separation,comminution and selection by winnowing. In this example, the heatcarrier was heated at the furnace and transported into the reactor. Thenthe heat carrier supplied a quantity of heat for the cracking process.The cracking gas can get combustible gas and oil by fractionating.What's more, the combustible gas, which was desulfurized by the sodiumhydroxide, can be directly expelled into or stored and then expelledinto the heating furnace for burning. Moreover, the temperature of theheat carrier can be adjusted at 400° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 68

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 47. Theactive alumina is 26 wt %, the zinc oxide is 13 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 420° C., thecracking time is 20 minutes and the heating temperature difference inthe cracking chamber is 2° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the sodium hydroxide, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. Moreover, the temperature of the heat carrier canbe adjusted at 450° C., which satisfy the temperature request forcracking. The rest parts exercise the same as the existing technologies.

EXAMPLE 69

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 36. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 8 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 385° C. and thecracking time is 40 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the sodium hydroxide, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. Moreover, the temperature of the heat carrier canbe adjusted at 405° C., which satisfy the temperature request forcracking. The rest parts exercise the same as the existing technologies.

EXAMPLE 70

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 37. Theactive alumina is 17 wt %, the zinc oxide is 10 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 6.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 390° C., thecracking time is 30 minutes and the heating temperature difference inthe cracking chamber is 7° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the sodium hydroxide, can bedirectly expelled into or stored and then expelled into the heatingfurnace for burning. Moreover, the temperature of the heat carrier canbe adjusted at 420° C., which satisfy the temperature request forcracking. The rest parts exercise the same as the existing technologies.

EXAMPLE 71

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 38. Theactive alumina is 25 wt %, the zinc oxide is 10 wt %, the active argilis 10 wt % and the kaoline is 5 wt %. The weight ratio of catalyst andrubber is 5.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 450° C., thecracking time is 10 minutes and the heating temperature difference inthe cracking chamber is 1° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the conventionaldesulfurization method, can be directly expelled into or stored and thenexpelled into the heating furnace for burning. The exhaust gas, makingby burning the combustible gas, should be treated again and exhaustedout. What's more, the secondary treating can adopt the following mode:refrigerating the exhaust gas below 40° C., then deal with it by thetransaction layer of active carbon, active fiber and zeolite molecularsieve, respectively. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 72

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C. and thecracking time is 80 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the conventionaldesulfurization method, can be directly expelled into or stored and thenexpelled into the heating furnace for burning. The exhaust gas, makingby burning the combustible gas, should be treated again and exhaustedout. What's more, the secondary treating can adopt the following mode:refrigerating the exhaust gas below 68° C., then deal with it by thetransaction layer of active carbon, active fiber and zeolite molecularsieve, respectively. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 73

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt %, the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C. and thecracking time is 50 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black by the procedure of magnetic separation, comminution andselection by winnowing. In this example, the heat carrier was heated atthe furnace and transported into the reactor. Then the heat carriersupplied a quantity of heat for the cracking process. The cracking gascan get combustible gas and oil by fractionating. What's more, thecombustible gas, which was desulfurized by the conventionaldesulfurization method, can be directly expelled into or stored and thenexpelled into the heating furnace for burning. The exhaust gas, makingby burning the combustible gas, should be treated again and exhaustedout. What's more, the secondary treating can adopt the following mode:refrigerating the exhaust gas below 65° C., then deal with it by thetransaction layer of active carbon, active fiber and zeolite molecularsieve, respectively, and the following rate of exhaust gas wascontrolled at 0.1 m/s. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 74

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 39. Theactive alumina is 19 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt %, the kaoline is 15 wt %. The weight ratio of catalyst andrubber is 3.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 370° C. and thecracking time is 60 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 700 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the sodium hydroxide, can be directly expelled into or stored andthen expelled into the heating furnace for burning. The exhaust gas,making by burning the combustible gas, should be treated again andexhausted out. What's more, the secondary treating can adopt thefollowing mode: refrigerating the exhaust gas below 64° C., then dealwith it by the transaction layer of active carbon, active fiber andzeolite molecular sieve, respectively, and the through speed of exhaustgas was controlled at 0.3 m/s. The rest parts exercise the same as theexisting technologies.

EXAMPLE 75

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 40. Theactive alumina is 29 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 3.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 420° C., thecracking time is 35 minutes and the heating temperature difference inthe cracking chamber is 8° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 750 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the sodium hydroxide, can be directly expelled into or stored andthen expelled into the heating furnace for burning. The exhaust gas,making by burning the combustible gas, should be treated again andexhausted out. What's more, the secondary treating can adopt thefollowing mode: refrigerating the exhaust gas below 50° C., then dealwith it by the transaction layer of active carbon, active fiber andzeolite molecular sieve, respectively, and the following rate of exhaustgas was controlled at 0.2 m/s. The rest parts exercise the same as theexisting technologies.

EXAMPLE 76

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 41. Theactive alumina is 28 wt %, the zinc oxide is 19 wt %, the active argilis 12 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 4:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 380° C. and thecracking time is 30 minutes. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 650 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the conventional desulfurization method, can be directly expelledinto or stored and then expelled into the heating furnace for burning.The exhaust gas, making by burning the combustible gas, should betreated again and exhausted out. What's more, the secondary treating canadopt the following mode: refrigerating the exhaust gas below 42° C.,then deal with it by the transaction layer of active carbon, activefiber and zeolite molecular sieve, respectively, and the through speedof exhaust gas was controlled at 0.4 m/s. The rest parts exercise thesame as the existing technologies.

EXAMPLE 77

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 42. Theactive alumina is 26 wt %, the zinc oxide is 11 wt %, the active argilis 10 wt % and the kaoline is 15 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 390° C., thecracking time is 30 minutes and the heating temperature difference inthe cracking chamber is 7° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 650 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the conventional desulfurization method, can be directly expelledinto or stored and then expelled into the heating furnace for burning.The exhaust gas, making by burning the combustible gas, should betreated again and exhausted out. What's more, the secondary treating canadopt the following mode: refrigerating the exhaust gas below 60° C.,then deal with it by the transaction layer of active carbon, activefiber and zeolite molecular sieve, respectively, and the following rateof exhaust gas was controlled at 0.6 m/s. The rest parts exercise thesame as the existing technologies.

EXAMPLE 78

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 35. Theactive alumina is 15 wt %, the zinc oxide is 10 wt %, the active argilis 5 wt % and the kaoline is 5 wt %. The weight ratio of catalyst andrubber is 6:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C., thecracking time is 60 minutes and the heating temperature difference inthe cracking chamber is 6□. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 700 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the conventional desulfurization method, can be directly expelledinto or stored and then expelled into the heating furnace for burning.The exhaust gas, making by burning the combustible gas, should betreated again and exhausted out. What's more, the secondary treating canadopt the following mode: refrigerating the exhaust gas below 40° C.,then deal with it by the transaction layer of active carbon, activefiber and zeolite molecular sieve, respectively, and the through speedof exhaust gas was controlled at 0.2 m/s. Moreover, the temperature ofthe heat carrier can be adjusted at 380° C., which satisfy thetemperature request for cracking. The rest parts exercise the same asthe existing technologies.

EXAMPLE 79

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 40. Theactive alumina is 18 wt %, the zinc oxide is 12 wt %, the active argilis 7 wt % and the kaoline is 11 wt %. The weight ratio of catalyst andrubber is 3:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 360° C., thecracking time is 75 minutes and the heating temperature difference inthe cracking chamber is 7° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 650 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the conventional desulfurization method, can be directly expelledinto or stored and then expelled into the heating furnace for burning.The exhaust gas, making by burning the combustible gas, should betreated again and exhausted out. What's more, the secondary treating canadopt the following mode: refrigerating the exhaust gas below 35° C.,then deal with it by the transaction layer of active carbon, activefiber and zeolite molecular sieve, respectively, and the following rateof exhaust gas was controlled at 0.7 m/s. Moreover, the temperature ofthe heat carrier can be adjusted at 400° C., which satisfy thetemperature request for cracking. The rest parts exercise the same asthe existing technologies.

EXAMPLE 80

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 4A, and the weight percentage is 45. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 350° C., thecracking time is 50 minutes and the heating temperature difference inthe cracking chamber is 2° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 750 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the sodium hydroxide, can be directly expelled into or stored andthen expelled into the heating furnace for burning. The exhaust gas,making by burning the combustible gas, should be treated again andexhausted out. What's more, the secondary treating can adopt thefollowing mode: refrigerating the exhaust gas below 58° C., then dealwith it by the transaction layer of active carbon, active fiber andzeolite molecular sieve, respectively, and the through speed of exhaustgas was controlled at 0.2 m/s. Moreover, the temperature of the heatcarrier can be adjusted between 380 and 490° C., which satisfy thetemperature request for cracking. The rest parts exercise the same asthe existing technologies.

EXAMPLE 81

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 5A, and the weight percentage is 44. Theactive alumina is 20 wt %, the zinc oxide is 15 wt %, the active argilis 8 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 6.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 370° C., thecracking time is 60 minutes and the heating temperature difference inthe cracking chamber is 1° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 650 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the sodium hydroxide, can be directly expelled into or stored andthen expelled into the heating furnace for burning. The exhaust gas,making by burning the combustible gas, should be treated again andexhausted out. What's more, the secondary treating can adopt thefollowing mode: refrigerating the exhaust gas below 45° C., then dealwith it by the transaction layer of active carbon, active fiber andzeolite molecular sieve, respectively, and the through speed of exhaustgas was controlled at 0.3 m/s. Moreover, the temperature of the heatcarrier can be adjusted at 405° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 82

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is 3A, and the weight percentage is 46. Theactive alumina is 25 wt %, the zinc oxide is 15 wt %, the active argilis 6 wt % and the kaoline is 9 wt %. The weight ratio of catalyst andrubber is 4.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 420° C., thecracking time is 25 minutes and the heating temperature difference inthe cracking chamber is 3° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 700 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the sodium hydroxide, can be directly expelled into or stored andthen expelled into the heating furnace for burning. The exhaust gas,making by burning the combustible gas, should be treated again andexhausted out. What's more, the secondary treating can adopt thefollowing mode: refrigerating the exhaust gas below 55° C., then dealwith it by the transaction layer of active carbon, active fiber andzeolite molecular sieve, respectively, and the following rate of exhaustgas was controlled at 0.1 m/s. Moreover, the temperature of the heatcarrier can be adjusted at 455° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 83

The components and weight percentage of the catalyzer are as following:the model of molecular sieve is Y, and the weight percentage is 47. Theactive alumina is 30 wt %, the zinc oxide is 19 wt %, the active argilis 10 wt % and the kaoline is 8 wt %. The weight ratio of catalyst andrubber is 2.5:1000, and then the mixture is transported into the reactorfor the cracking reaction. The cracking temperature is 380° C., thecracking time is 40 minutes and the heating temperature difference inthe cracking chamber is 5° C. The liquid state product can be made intoneeding oil by fractionating. Moreover, the solid state product, whichproduced after cracking, contains carbon black. And it can be made intocarbon black, which can pass the screen of 650 mesh, by the procedure ofmagnetic separation, comminution and selection by winnowing. In thisexample, the heat carrier was heated at the furnace and transported intothe reactor. Then the heat carrier supplied a quantity of heat for thecracking process. The cracking gas can get combustible gas and oil byfractionating. What's more, the combustible gas, which was desulfurizedby the sodium hydroxide, can be directly expelled into or stored andthen expelled into the heating furnace for burning. The exhaust gas,making by burning the combustible gas, should be treated again andexhausted out. What's more, the secondary treating can adopt thefollowing mode: refrigerating the exhaust gas below 48° C., then dealwith it by the transaction layer of active carbon, active fiber andzeolite molecular sieve, respectively, and the through speed of exhaustgas was controlled at 0.4 m/s. Moreover, the temperature of the heatcarrier can be adjusted at 415° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

EXAMPLE 84

The steel wires were separated from rubber by drawing the waste rubberinto thread, and then the big pieces of rubber were broken up intogranule. What's more, the components and weight percentage of thecatalyzer are as following: the model of molecular sieve is Y, and theweight percentage is 50. The active alumina is 29 wt %, the zinc oxideis 20 wt %, the active argil is 15 wt % and the kaoline is 15 wt %. Theweight ratio of catalyst and rubber is 2:1000, and then the mixture istransported into the reactor for the cracking reaction. The crackingtemperature is 390° C., the cracking time is 30 minutes, and the heatingtemperature difference in the cracking chamber is 2° C. And the hotmolten salt is the best heat carrier. The cracking gas was input intofractionating tower. Moreover, the combustible gas was purified by thesodium hydroxide desulfurization, and stored as the fuel for the heatcarrier heater. The liquid state products, which fractionated from thecracking gas, can be made into the needing oil and stored. What's more,the solid state product, which produced after cracking, contains carbonblack. And it can be made into carbon black, which can pass the screenof 650 mesh, by the procedure of magnetic separation, comminution andselection by winnowing. After accomplishing the aforementioned process,the high strength and rarefied carbon black can be gained by adding thestearic acid into the carbon black, that's because the zinc stearate canreinforce the role of carbon black. In this example, the heat carrierwas heated at the furnace and transported into the reactor. Then theheat carrier supplied a quantity of heat for the cracking process. Theexhaust gas, making by burning the combustible gas, should be treatedagain and exhausted out. What's more, the secondary treating can adoptthe following mode: refrigerating the exhaust gas below 50° C., thendeal with it by the transaction layer of active carbon, active fiber andzeolite molecular sieve, respectively, and the following rate of exhaustgas was controlled at 0.1 m/s. Moreover, the temperature of the heatcarrier can be adjusted at 420° C., which satisfy the temperaturerequest for cracking. The rest parts exercise the same as the existingtechnologies.

The waste rubber was treated by the cracking technology as the example84 mentioned, and the contrast of the correlative parameter of theproduct between the example 84 and the existing technology is asfollowing:

1. The weight percentage of the final product, which is attained by theexisting technology, is as following: the fuel is from 31 to 36, thecarbon black is 38, the steel wire is 11 and the combustible gas is from15 to 20.

The weight percentage of the final product, which is attained by thetechnology of this example, is as following: the fuel is 48, the carbonblack is 38, the steel wire is 11 and the combustible gas is 3.

The steel wire and carbon black are not molar losing in the crackingprocess of this example, thus it can be seen that the use of the wasterubber cracking technology, as this example mentioned, can greatlyimprove the proportion of the fuel in the final product, and can attainthe optimal producing effect. What's more, the use of the lowtemperature in the cracking process makes the temperature in the wholecracking process is equally below 450□, which saving abundant energysources and attaining the optimal cost-effective ratio.

2. The reinforced carbon black, which attained by the technology of thisexample mentioned, is detected by the carbon black detection methodwhich accords with the national institute of standards. And theidiographic capability of this carbon black is as following: the rubberadding with the reinforced carbon black was sulfurated on the standardsulfuration condition, which is 145□ and 30 minutes. The elongationratio of the product is 428%, the tensile strength is 22.8 Mpa, the 300%stretching intensity is 13.6 Mpa, and the rigidity is 69SH. What's more,the other indexes are according or exceeding the national institute ofstandards. However, the chemical character of the carbon black waschanged because of the high cracking temperature using in the existingtechnology. So the indexes are hard to reach this standard.

3. The combustible gas can be disposed by the existing technology andthe optimal indexes are as following: the concentration of the smokeemission is 300 mg/m³, the concentration of the plumbum emission is 0.5mg/m³, the concentration of the hydrochloric emission is 50 mg/m³, theconcentration of the benzene emission is 70 mg/m³, the concentration ofthe toluene emission is 50 mg/m³, the concentration of thedimethylbenzene emission is 5 mg/m³, the concentration of theformaldehyde emission is 1 mg/m³, the concentration of the hydrargyrumemission is 0.6 mg/m³, the concentration of the fluoride emission is 20mg/m³, the concentration of the sulfur dioxide emission is 400 mg/m³,the concentration of the carbon monoxide emission is 150 mg/m³, theconcentration of the nitrogen oxides emission is 600 mg/m³, theconcentration of the sulfureted hydrogen emission is 50 mg/m³, theconcentration of the dioxin emission is 20 ng/m³.

In this example, the exhaust gas, which attained by burning thecombustible gas in furnace, was treated with a second purifyingtechnology. And the letting standards of the contamination of thisexample are reaching a lowest level, which completely attain theinternational request for the environmental protection. The detectingresults are as the table 1 showing.

Comparing the detecting results between this example and the existingtechnology, and using the cracking technology and the followingpurificatory technology of this invention, it is obvious that theindexes of the exhaust gas, which attained by burning the combustiblegas in furnace, are best. What's more, it can farthest reduce theenvironmental pollution and reach a win-win situation between theinterest and the environmental benefit.

TABLE 1 The number of laboratory 6110003- 6110003- 6110003- 01 02 03 Theidentification of pattern Discharge Discharge Discharge side 1-1 side1-2 side 1-3 The sampling date Nov. 02, 2006 Nov. 02, 2006 Nov. 02, 2006The incepting date of pattern Nov. 02, 2006 Nov. 02, 2006 Nov. 02, 2006The The The exhaust exhaust exhaust The analysis index The means Theunits gas gas gas The smoke The GB5468-1991 % 2.02 humidity content TheGB/T16157-1966 mg/m3 0.32 0.039 0.0025 emission concentration The kg/h1.42 × 10⁻⁴ emission speed Cadmium The 1) mg/m3 <0.008 <0.008 <0.008emission concentration The kg/h 4.36 × 10⁻⁴ emission speed PlumbumThe 1) mg/m3 <0.08 0.116 <0.08 emission concentration The kg/h 4.36 ×10⁻⁵ emission speed Hydrogen The 1) mg/m3 <0.8 <0.8 <0.8 Chlorideemission concentration The kg/h 4.36 × 10⁻⁴ emission speed Benzene TheGB/T14677-1993 mg/m3 <0.06 <0.06 <0.06 emission concentration The kg/h2.91 × 10⁻⁵ emission speed Toluene The GB/T14677-1993 mg/m3 <0.06 <0.06<0.06 emission concentration The kg/h 2.91 × 10⁻⁵ emission speedDimethylbenzene The GB/T14677-1993 mg/m3 <0.06 <0.06 <0.06 emissionconcentration The kg/h 2.91 × 10⁻⁵ emission speed Formaldehyde TheGB/T15516-1995 mg/m3 <0.18 <0.18 <0.18 emission concentration The kg/h1.02 × 10⁻⁴ emission speed Hydrargyrum The 2) mg/m3 <0.01 <0.01 0.02emission concentration The kg/h 7.27 × 10⁻⁴ emission speed Fluoride TheHJ/T67-2001 mg/m3 0.79 0.81 0.79 emission concentration The kg/h 8.72 ×10⁻⁴ emission speed Sulfur Dioxide The HJ/T57-2000 mg/m3 <3.0 <3.0 <3.0emission concentration The kg/h 1.45 × 10⁻³ emission speed Carbon The 1)mg/m3 39.4 31.6 26.3 Monoxide emission concentration The kg/h 0.036emission speed Nitrogen The 1) mg/m3 62.6 53.6 31.3 Dioxide emissionconcentration The kg/h 0.054 emission speed Sulfureted The 1) mg/m3 1.603.91 9.18 Hydrogen emission concentration The kg/h 6.33 × 10⁻³ emissionspeed Dioxin The EPA Method23 ng/m3 0.00240 emission concentration

1. A method for cracking waste rubber, the method comprising: adding arubber mass and a catalyst in a cracking chamber of a cracking reactorand cracking said rubber mass at a temperature ranging from 350 to 450°C., wherein the catalyst comprises a mixture of 35 to 50 wt %aluminosilicate, 15 to 30 wt % active alumina, 10 to 20 wt % zinc oxide,5 to 15 wt % active argil, and 5 to 15 wt % kaolin, and is present inthe cracking reactor in a weight ratio of 2-7:1000 catalyst:rubber mass.2. The method of claim 1, wherein a heating temperature difference inthe cracking chamber is less than or equal to 10° C.
 3. The method ofclaim 1, wherein cracking time ranges from 20 to 60 minutes.
 4. Themethod of claim 1, wherein cracking temperature ranges from 370 to 420°C.
 5. The method of claim 4, wherein the cracking temperature rangesfrom 380 to 390° C.
 6. The method of claim 1, further comprisingsupplying heat to the cracking chamber by a temperature controlled heatcarrier, a heating temperature of the heat carrier ranging from 380 to490° C.
 7. The method of claim 1, further comprising: heating a heatcarrier via a furnace; transporting the heat carrier into the reactor,the heat carrier supplying a quantity of heat for the cracking; andfractionating a cracking gas to produce combustible gas and oil, whereinthe combustible gas is desulfurized and either directly expelled into orstored and then expelled into the furnace for burning.
 8. The method ofclaim 7, wherein exhaust gas produced by burning the combustible gas, istreated via a secondary treatment and exhausted out, the secondarytreating comprising refrigerating the exhaust gas below 70° C. andprocessing a transaction layer of active carbon, active fiber, and azeolite molecular sieve.
 9. The method of claim 8, wherein a temperatureof the exhaust gas is at least initially below from 40 to 55° C. duringthe secondary treatment.
 10. The method of claim 8, wherein throughputduring the secondary treatment of the exhaust gas is controlled between0.1 and 1 m/s.
 11. The method of claim 1, wherein a solid state product,produced after said cracking, contains carbon black, the carbon blackbeing produced by magnetic separation, comminution, and selection bywinnowing.
 12. The method of claim 11, further comprising after thesolid state product is produced, adding stearic acid into the carbonblack, so as to produce zinc stearate from the stearic acid and zincoxide and to reinforce the role of carbon black.